WO2020171008A1 - Procédé de fonctionnement d'un haut-fourneau - Google Patents

Procédé de fonctionnement d'un haut-fourneau Download PDF

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Publication number
WO2020171008A1
WO2020171008A1 PCT/JP2020/006011 JP2020006011W WO2020171008A1 WO 2020171008 A1 WO2020171008 A1 WO 2020171008A1 JP 2020006011 W JP2020006011 W JP 2020006011W WO 2020171008 A1 WO2020171008 A1 WO 2020171008A1
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WIPO (PCT)
Prior art keywords
reducing gas
carbon
blast furnace
gas
correlation
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Ceased
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PCT/JP2020/006011
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English (en)
Japanese (ja)
Inventor
酒井　博
浩樹 西岡
中野　薫
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JFE Steel Corp
Kobe Steel Ltd
Nippon Steel Corp
Nippon Steel Engineering Co Ltd
Original Assignee
JFE Steel Corp
Kobe Steel Ltd
Nippon Steel Corp
Nippon Steel Engineering Co Ltd
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Application filed by JFE Steel Corp, Kobe Steel Ltd, Nippon Steel Corp, Nippon Steel Engineering Co Ltd filed Critical JFE Steel Corp
Priority to EP20759676.8A priority Critical patent/EP3907303B1/fr
Priority to ES20759676T priority patent/ES2981767T3/es
Priority to CA3128163A priority patent/CA3128163C/fr
Priority to BR112021014817-5A priority patent/BR112021014817A2/pt
Priority to AU2020226229A priority patent/AU2020226229B2/en
Priority to UAA202104860A priority patent/UA127367C2/uk
Priority to US17/430,657 priority patent/US12180555B2/en
Priority to CN202080014651.XA priority patent/CN113423845B/zh
Priority to KR1020217027226A priority patent/KR102585689B1/ko
Publication of WO2020171008A1 publication Critical patent/WO2020171008A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/006—Automatically controlling the process
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/001—Injecting additional fuel or reducing agents
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/06—Making pig-iron in the blast furnace using top gas in the blast furnace process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B14/00—Crucible or pot furnaces
    • F27B14/08—Details specially adapted for crucible or pot furnaces
    • F27B14/14—Arrangements of heating devices
    • F27B14/143—Heating of the crucible by convection of combustion gases
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/001—Injecting additional fuel or reducing agents
    • C21B2005/005—Selection or treatment of the reducing gases
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2300/00—Process aspects
    • C21B2300/04—Modeling of the process, e.g. for control purposes; CII
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]

Definitions

  • the present invention relates to a blast furnace operating method.
  • the present application claims priority based on Japanese Patent Application No. 2019-26220 filed in Japan on February 18, 2019, and the content thereof is incorporated herein.
  • the blast furnace method is the mainstream of the pig iron manufacturing process.
  • iron-based raw materials for blast furnace raw materials containing iron oxide. Mainly sinter ore; hereinafter also simply referred to as "iron-based raw materials”
  • coke are loaded from the top of the blast furnace alternately and in layers.
  • hot air is blown into the blast furnace from the tuyere at the bottom of the blast furnace.
  • the hot air reacts with the pulverized coal blown together with the hot air and the coke in the blast furnace to generate a high-temperature reducing gas (here mainly CO gas) in the blast furnace. That is, the hot air gasifies the coke and the pulverized coal in the blast furnace.
  • a high-temperature reducing gas here mainly CO gas
  • the reducing gas rises in the blast furnace and reduces the iron-based raw material while heating it.
  • the iron-based raw material is heated and reduced by the reducing gas while descending in the blast furnace. Then, the iron-based raw material is melted and dropped inside the blast furnace while being further reduced by coke.
  • the iron-based raw material is finally stored in the hearth as hot metal (pig iron) containing less than 5% by mass of carbon.
  • the hot metal in the hearth is taken out from the tap hole and subjected to the next steelmaking process. Therefore, in the blast furnace method, carbonaceous materials such as coke and pulverized coal are used as reducing agents.
  • the reducing agent ratio is specifically the coke and pulverized coal required to produce 1 ton of hot metal (and the reducing gas blown from the tuyere when the reducing gas is blown from the tuyere (described later)). ) Is the total mass.
  • the reducing material has a role of becoming heat in the furnace to raise the temperature of the charging material and a role of reducing the iron-based raw material in the furnace.
  • the reduction reaction in the furnace can be expressed by various reaction formulas.
  • the direct reduction reaction with coke reaction formula: FeO+C ⁇ Fe+CO
  • reaction formula: FeO+C ⁇ Fe+CO is an endothermic reaction with a large endotherm. Therefore, it is important to minimize the direct reduction reaction in reducing the reducing material ratio. This is because if the direct reduction reaction is not generated, the amount of coke required for the direct reduction reaction and the amount of the reducing material used as a heat source can be reduced.
  • this direct reduction reaction occurs in the lower part of the blast furnace, if the iron-based raw material can be sufficiently reduced by the reducing gas such as CO or H 2 before the iron-based raw material reaches the lower part of the furnace, the direct reduction reaction
  • the target iron-based raw materials can be reduced.
  • the blowing amount of the reducing gas containing carbon (the blowing amount per ton of hot metal)
  • the amount of carbon fed into the blast furnace also increases as the blowing amount increases.
  • the CO gas utilization rate of the blast furnace changes as the amount of reducing gas blown in increases, but if the amount of reducing gas blown in is excessively increased, a large amount of reducing gas is discharged without being used in the furnace. Will be done. Therefore, simply increasing the blowing amount of the reducing gas causes the carbon in the reducing gas to be discharged without being used for the reduction, so that the ratio of the reducing material increases or the CO 2 emission amount increases. there is a possibility.
  • the present invention has been made in view of the above problems, and an object of the present invention is to provide a new and improved blast furnace operating method capable of obtaining a desired reducing agent ratio reduction effect. To do.
  • the present inventor first defined a parameter called the reduction amount Input ⁇ C of the carbon consumption basic unit by blowing the reducing gas into the blast furnace.
  • the carbon consumption basic unit Input C (kg/t-pig) is the amount of carbon consumed per ton (t-pig) of hot metal, more specifically, the coke and the coke required to produce 1 ton of hot metal.
  • the total mass of pulverized coal and carbon contained in the reducing gas blown from the tuyere. Input C is specifically calculated by the following mathematical expression (1).
  • Input C (kg/t-pig) coke ratio (kg/t-pig) x carbon ratio in coke (mass %) + pulverized coal ratio (kg/t-pig) x carbon ratio in pulverized coal (mass%) ) + Reduction gas consumption rate (Nm 3 /t-pig) ⁇ carbon ratio in reduction gas (kg/Nm 3 ) (1)
  • the coke ratio and the pulverized coal ratio are the amounts of coke and pulverized coal used per ton of hot metal, respectively.
  • the basic amount of reducing gas used is the amount of reducing gas blown in per ton of hot metal.
  • the carbon ratio in the coke is the mass% of carbon with respect to the total mass of the coke
  • the carbon ratio in the pulverized coal is the mass% of carbon with respect to the total mass of the pulverized coal.
  • the carbon ratio in the reducing gas is the carbon content per unit volume of the reducing gas.
  • the basic unit of the amount of reducing gas used is the volume (Nm 3 /t-pig) of the reducing gas blown to produce 1 ton of hot metal
  • the carbon ratio in the reducing gas is the unit of the reducing gas.
  • the carbon content per volume (kg/Nm 3 ) was used, but the basic unit of the amount of reducing gas used was the mass of reducing gas blown to produce 1 ton of hot metal (kg/t-pig).
  • the carbon ratio may be a mass% of carbon with respect to the total mass of the reducing gas.
  • Input ⁇ C can be defined as, for example, a reduction rate (percentage, %) of the carbon consumption basic unit (Input C) with respect to the base operation in the operation in which a predetermined amount of reducing gas is blown.
  • As the base operation for example, an operation condition in which the reducing gas is not blown can be set. If Input C of the base operation is A (kg/t-pig) and Input C in the operation of blowing a predetermined amount of reducing gas is B (kg/t-pig), Input ⁇ C is given by the following formula (2). Shown.
  • the reduction amount Input ⁇ C of the carbon consumption basic unit is not limited to that shown in the following mathematical expression (2), and may be a value indicating the degree of reduction of the carbon consumption basic unit with respect to the base operation.
  • Input ⁇ C may be the difference between A and B (AB).
  • Input ⁇ C (AB)/A ⁇ 100(%) (2)
  • Input ⁇ C is a parameter corresponding to the reducing agent ratio, and the larger the Input ⁇ C, the greater the reduction amount of the reducing agent ratio with respect to the base operation. Then, the inventor performs a blast furnace operation simulation by changing the type of the reducing gas and the blowing amount (the blowing amount per 1 ton of hot metal), as described in detail in Examples below, and performs a plurality of reducing gases. Input ⁇ C was calculated with respect to the blowing amount. As a result, while the reducing gas blowing amount is small, the Input ⁇ C increases as the blowing amount increases, but as the reducing gas blowing amount is further increased, the input ⁇ C increase amount decreases. However, it became clear that it would eventually decline.
  • the present inventor examined parameters that affect the Input ⁇ C or the reducing agent ratio.
  • the present inventor focused on the amount of hydrogen input (Nm 3 /t-pig) into the blast furnace per ton of hot metal.
  • Hydrogen here refers to hydrogen that is put in front of the tuyere, and in addition to hydrogen contained in the reducing gas, hydrogen in blast moisture and hydrogen in pulverized coal are also included.
  • the present inventor changes the hydrogen input amount by changing the type of the reducing gas and the injection amount, and obtains the correlation between the hydrogen input amount and the hydrogen reduction rate (%) at this time by the blast furnace operation simulation. It was Here, the blast furnace operation simulation was performed by the same method as in Example 1 described later.
  • the hydrogen reduction rate is defined as the proportion of iron oxide charged into the furnace that is reduced by hydrogen, and the CO reduction rate (rate reduced by CO gas) and the direct reduction rate (direct reduction with C). And the total of 100%).
  • coke oven gas (COG), natural gas (NG), and a mixed gas of coke oven gas and hydrogen gas were used as the reducing gas.
  • the inventor of the present invention focused on the basic unit of carbon brought into the blast furnace by the reducing gas blown from the tuyere.
  • the basic unit of carbon brought into the blast furnace by the reducing gas is obtained by multiplying the injection amount of the reducing gas per ton of hot metal (Nm 3 /t-pig) by the carbon ratio in the reducing gas (kg/Nm 3 ). This is the value that can be obtained.
  • the basic unit of carbon brought into the blast furnace by the reducing gas is also simply referred to as “the basic unit of carbon in the reducing gas”.
  • the inventor changed the carbon intensity and the type of the reducing gas in the reducing gas to carry out a blast furnace operation simulation to calculate Input ⁇ C, as described in detail in Examples below.
  • the present inventor has found that there is a correlation between Input ⁇ C and the carbon intensity in the reducing gas.
  • the correlation between Input ⁇ C and the carbon intensity in the reducing gas was found to be that of carbon atoms and hydrogen in the reducing gas. It was clarified that different tendencies were exhibited when the molar ratio C/H with the atom was 0.15 or more and when it was less than 0.15. More specifically, when the C/H of the reducing gas is 0.15 or more, the correlation between Input ⁇ C and the carbon intensity in the reducing gas does not depend on the type of the reducing gas (in other words, It is uniquely determined (regardless of the reducing gas C/H).
  • the correlation between the Input ⁇ C and the carbon intensity of the reducing gas differs for each C/H of the reducing gas.
  • the correlation between Input ⁇ C and the carbon intensity in the reducing gas is shown by a graph having a convex curve (that is, the carbon intensity in the reducing gas has a certain value). Shows the maximum value).
  • the Input ⁇ C can be set to a predetermined target based on the correlation.
  • the carbon intensity in the reducing gas can be determined so as to be equal to or higher than the value.
  • the blowing amount of the reducing gas blown into the blast furnace can be adjusted based on the determined carbon basic unit in the reducing gas and the carbon ratio in the reducing gas.
  • a desired Input ⁇ C that is, Input ⁇ C equal to or larger than the target value
  • Input ⁇ C shows a maximum value when the carbon intensity in the reducing gas has a certain value (detailed graph will be described later). Therefore, if the carbon intensity in the reducing gas is determined around this maximum value, the reducing agent ratio can be reduced more efficiently. Furthermore, if the above correlation is obtained for each C/H of the reducing gas, then the injection amount of the reducing gas can be determined based on the above correlation according to the C/H of the reducing gas. The present inventor has completed the present invention based on such findings.
  • the gist of the present invention is as follows.
  • a blast furnace operating method in which a reducing gas containing hydrogen atoms and carbon atoms is blown into a blast furnace, wherein the molar ratio of carbon atoms to hydrogen atoms in the reducing gas is C/H.
  • the step of obtaining the correlation between the carbon intensity in the reducing gas and the amount of reduction in the carbon consumption intensity due to the injection of the reducing gas into the blast furnace, Input ⁇ C, and the correlation obtained for each C/H Based on this, a step of determining the carbon intensity in the reducing gas that becomes equal to or larger than the target value of the reduction amount Input ⁇ C of the predetermined carbon consumption intensity, the determined carbon intensity in the reducing gas, and the reducing gas And a step of adjusting the blowing amount of the reducing gas blown into the blast furnace on the basis of the carbon content in the blast furnace.
  • the molar ratio C/H of carbon atoms and hydrogen atoms of the reducing gas may be 0.15 or more.
  • the correlation may be expressed by a quadratic expression of carbon intensity in reducing gas.
  • the carbon intensity in the reducing gas may be determined within the range of 21 to 107 kg/t-pig.
  • the carbon intensity in the reducing gas may be determined within the range of 21 to 65 kg/t-pig.
  • the molar ratio C/H of carbon atoms and hydrogen atoms in the reducing gas may be more than 0 and less than 0.15.
  • the molar ratio C/H of carbon atoms and hydrogen atoms in the reducing gas may be 0.13 or less.
  • the molar ratio C/H of carbon atoms and hydrogen atoms in the reducing gas may be 0.10.
  • the pre-tuyere temperature may be adjusted to 2000°C or higher when the reducing gas is blown into the blast furnace.
  • At least one or more of the amount of air blown in the hot air and the oxygen enrichment ratio may be adjusted.
  • the reducing gas is selected from the group consisting of coke oven gas, natural gas, reformed top gas (BFG), city gas, mixed gas thereof, and hydrogen mixed gas in which hydrogen gas is mixed. May be done.
  • 6 is a graph showing a correlation between Input ⁇ C and carbon basic unit (kg/t-pig) in reducing gas for each C/H of reducing gas.
  • 3 is a graph showing the relationship between the hydrogen reduction rate and the hydrogen input amount (Nm 3 /t-pig) into the blast furnace per ton of hot metal.
  • 3 is a graph showing the relationship between the direct reduction rate and the hydrogen input amount (Nm 3 /t-pig) into the blast furnace per ton of hot metal.
  • the numerical limit range represented by “to” means a range including the numerical values before and after “to” as the lower limit value and the upper limit value. Numerical values indicating “above” or “less than” are not included in the numerical range.
  • Input ⁇ C can be defined as a reduction ratio of the carbon consumption basic unit due to the blowing of the reducing gas into the blast furnace, as described above.
  • Input C of the base operation is A (kg/t-pig) and Input C in the operation of blowing a predetermined amount of reducing gas is B (kg/t-pig)
  • the Input ⁇ C is not limited to that shown in the following mathematical expression (2), and the difference between A and B (AB) may be used as the Input ⁇ C.
  • Input ⁇ C (AB)/A ⁇ 100(%) (2)
  • the carbon basic unit in the reducing gas is the basic unit of carbon brought into the blast furnace by the reducing gas blown from the tuyere, and the blowing amount of the reducing gas per ton of hot metal (Nm 3 /t-pig ) Is multiplied by the carbon ratio (kg/Nm 3 ) in the reducing gas.
  • the reducing gas is blown into the blast furnace through tuyere provided in the blast furnace.
  • the reducing gas contains a reducing component that reduces the iron-based raw material in the blast furnace.
  • the reducing component of the present embodiment is not only a component capable of reducing the iron-based raw material itself (for example, CO gas, hydrogen gas) but also a reaction in the blast furnace (for example, coke, pulverized coal, etc.). (Eg, CO 2 gas, hydrocarbon gas, etc.) that can generate a reducing gas by the reaction or decomposition of
  • the ⁇ C-reducing gas correlation shown in FIG. 1 is created, for example, by performing a blast furnace operation simulation.
  • a blast furnace operation simulation for example, Koji TAKATANI, Takanobu INADA, Yutaka UJISAWA, “Three-dimensional Dynamic for Blast Furnace”, ISIJ International, V.I. 39 (1999), No. 1, p.
  • a so-called "blast furnace mathematical model” shown in 15-22 and the like can be used.
  • This blast furnace mathematical model roughly defines multiple meshes (small areas) by dividing the internal area of the blast furnace in the height direction, the radial direction, and the circumferential direction, and simulates the behavior of each mesh. is there.
  • the outline of the blast furnace operation simulation is as follows.
  • the blast furnace operation simulation is performed in various cases in which the C/H of the reducing gas and the blowing amount (the blowing amount per ton of hot metal) are different.
  • This case also includes the base operation (case in which the amount of reducing gas blown is 0).
  • the operating conditions are adjusted so that the front tuyere temperature and the hot metal temperature are as constant as possible between the cases. For example, at least one of the amount of air blown in the hot air and the oxygen enrichment ratio may be adjusted.
  • the pre-tuyere temperature is the temperature inside the furnace at the tip of the tuyere inside the furnace, and is also referred to as the tuyere tip temperature.
  • the temperature before the tuyere is calculated as the theoretical burning temperature at the tuyere according to the ram formula described in "Handbook of Ironmaking” (Ajijin Shokan) by Akitoshi Shigemi.
  • the hot air blown into the blast furnace is a gas containing air.
  • the hot air may further contain moisture and enriched oxygen in addition to air.
  • At least one of the coke ratio and the pulverized coal ratio may be adjusted.
  • the input ⁇ C and the carbon intensity in the reducing gas are calculated for each case.
  • the points indicating the Input ⁇ C and the carbon intensity in the reducing gas in each case are plotted on the xy plane shown in FIG.
  • Points P1 to P8 are examples of plotted points.
  • the approximation curve of each plot is obtained by an approximation method such as the least square method.
  • These approximate curves are graphs showing the ⁇ C-reducing gas correlation.
  • Graphs L1 to L5 are examples of graphs showing the ⁇ C-reducing gas correlation.
  • the correlation between the Input ⁇ C and the carbon intensity in the reducing gas that is, the ⁇ C-reducing gas correlation is that the molar ratio C/H of carbon atoms and hydrogen atoms in the reducing gas is 0.
  • the ⁇ C-reducing gas correlation when the C/H is 0.15 or more will be described.
  • Points P1 to P3 were determined by the same method as in Example 1 described later.
  • Point P4 was determined by the same method as in Example 1 except that the tuyere temperature was 2085°C or 2315°C.
  • a graph L1 is a graph showing an approximate curve of the points P1 to P4, that is, a ⁇ C-reducing gas correlation.
  • Examples of the reducing gas having a C/H of 0.15 or more include COG, natural gas, and city gas.
  • the reducing gas may be a gas obtained by reforming the furnace top exhaust gas (BFG) (a gas obtained by removing steam and CO 2 gas from the furnace top exhaust gas).
  • BFG furnace top exhaust gas
  • reducing gas containing hydrocarbon gas that is, COG, natural gas, city gas, and the like are preferable.
  • the hydrocarbon gas burns in the furnace to generate heat of combustion, so that further reduction of the reducing material ratio can be expected.
  • COG in a steel mill having a coke oven, it is possible to cover the energy in-house by using COG, and the cost is superior to that of other reducing gas, so COG is more preferable.
  • the upper limit of C/H is not particularly limited, but may be 0.3 or less, for example.
  • the composition of COG used in obtaining the data of points P2 and P4 is shown in Table 1, and the composition of the natural gas used in obtaining the data of point P3 is shown in Table 2. These compositions are measured by gas chromatography, a mass spectrometer or the like.
  • the numerical value of each component in Tables 1 and 2 is a molar ratio (more specifically, a molar concentration (mol/L) ratio).
  • C represents the carbon ratio (kg/Nm 3 ) in the reducing gas.
  • the C/H of COG having the composition shown in Table 1 below is 0.185.
  • the C/H of natural gas having the composition shown in Table 2 below is 0.271.
  • points P1 to P4 lie on substantially the same graph L1. Therefore, regardless of the type of the reducing gas (in other words, regardless of the C/H of the reducing gas), if the carbon basic unit in the reducing gas is obtained, Input ⁇ C is uniquely specified. That is, there is a correlation that does not depend on C/H between Input ⁇ C and the carbon intensity unit in the reducing gas, and the correlation is shown by the graph L1. Further, considering that the point P4 is also on the graph L1, it can be said that the correlation does not depend on the front tuyere temperature.
  • the graph L1 is a convex graph, it is represented by a quadratic equation of the carbon intensity in the reducing gas.
  • X is a carbon unit in the reducing gas
  • Y is Input ⁇ C.
  • the coefficients a1, b1 and c1 are all values that do not depend on the molar ratio C/H.
  • the graph L1 is not limited to that shown by this mathematical formula.
  • Input ⁇ C has a positive correlation with the carbon intensity in the reducing gas in the range where the carbon intensity in the reducing gas is 65 kg/t-pig or less, and the carbon intensity in the reducing gas is When the unit exceeds 65 kg/t-pig, it has a negative correlation with the carbon intensity in the reducing gas. Further, Input ⁇ C shows a maximum value when the carbon consumption rate in the reducing gas is about 65 kg/t-pig. Therefore, if the carbon intensity in the reducing gas is determined in the vicinity of this maximum value, the reducing agent ratio can be further reduced.
  • the Input ⁇ C is about 4.0% or more in the range where the carbon consumption rate in the reducing gas is 21 to 107 kg/t-pig.
  • the reducing agent ratio of the base operation is 375 to 500 kg/t-pig
  • the reducing agent ratio is reduced by approximately 15 to 20 kg/t-pig or more. This reduction amount is a significant value even considering the daily fluctuation of the reducing agent ratio, and the effectiveness of reducing the reducing agent ratio can be expected. Therefore, the carbon consumption rate in the reducing gas is preferably 21 to 107 kg/t-pig.
  • the maximum value is shown when the carbon intensity in the reducing gas is about 65 kg/t-pig, and when it exceeds 65 kg/t-pig, Input ⁇ C starts to decrease. In other words, the reduction effect of Input C is reduced.
  • the reason for this is that the carbon intensity in the reducing gas is over-supplied compared to the amount required for in-reactor reduction, which reduces the gas utilization rate.
  • the blowing amount also increases, the oxygen enrichment rate increases as the reducing gas blowing amount increases under the condition that the temperature before the tuyere is constant, and the amount of gas blown into the blast furnace via the hot stove decreases and the sensible heat of the blast is reduced. It can be considered that there is a decrease.
  • the carbon consumption rate in the reducing gas is more preferably 65 kg/t-pig or less, that is, 21 to 65 kg/t-pig.
  • Input ⁇ C can be increased (specifically, 4.0% or more) with a smaller amount of reducing gas blown.
  • a reducing gas having a low carbon ratio (kg/Nm 3 ) in the reducing gas (particularly, a reducing gas having a carbon ratio of less than 0.6 kg/Nm 3 ) is used, reduction may occur due to operational restrictions. In some cases, it is preferable to set the carbon consumption rate in the gas to 65 kg/t-pig or less. Hereinafter, the reason will be described in detail.
  • the pre-tuyere temperature In blast furnace operation, it is necessary to maintain the pre-tuyere temperature at a predetermined value or more as much as possible (here, the predetermined value may vary due to various factors, but it is often around 2000° C.). is there. If the temperature before the tuyere falls below the specified value, the combustibility of the pulverized coal decreases, and unburned char is generated, which obstructs ventilation in the furnace.Only a portion of the pulverized coal added as a reducing material (in the furnace This is because it causes a problem that it cannot be used as a reducing gas (generated).
  • the carbon unit in the reducing gas is 83 kg/t-pig
  • the front tuyere temperature can be maintained at a predetermined value or higher.
  • the front tuyere temperature is extremely close to a predetermined value, and it is necessary to carefully design operating specifications and to carefully monitor the operation. Therefore, the operation is possible, but the operation requires time and effort.
  • the carbon unit consumption in the reducing gas is 95 kg/t-pig, it is necessary to blow COG at 400 Nm 3 /t-pig.
  • the carbon consumption rate in the reducing gas is 65 kg/t-pig or less, the COG blowing rate can be made even lower than 350 Nm 3 /t-pig. You can afford it. Therefore, when a reducing gas having a low carbon ratio (kg/Nm 3 ) in the reducing gas (particularly, a reducing gas having a carbon ratio of less than 0.6 kg/Nm 3 ) is used, the carbon basic unit in the reducing gas is 65 kg/ It is preferably t-pig or less.
  • the above limitation does not basically occur.
  • the carbon consumption rate in the reducing gas is 100 kg/t-pig, which is much larger than 65 kg/t-pig, the blowing amount of the reducing gas is about 170 Nm 3 /t-pig.
  • the carbon consumption rate in the reducing gas can be made larger than 65 kg/t-pig.
  • the point P2 is plotted in the range of 65 kg/t-pig or less, while the point P3 is plotted in a wider range.
  • point P5 indicates Input ⁇ C and carbon intensity in the reducing gas when C/H of the reducing gas is 0.054, and point P6 is when C/H of the reducing gas is 0.097.
  • Input ⁇ C and carbon intensity in reducing gas point P7 indicates Input ⁇ C and carbon intensity in reducing gas when C/H of reducing gas is 0.137, and point P8 is reduction.
  • the input ⁇ C and the carbon intensity in the reducing gas when the C/H of the gas is 0.02 are shown.
  • Points P5 to P8 were determined by the same method as in Example 2 described later.
  • Graphs L2 to L5 are approximate curves of points P5 to P8, that is, graphs showing the ⁇ C-reducing gas correlation.
  • the reducing gas having a C/H of less than 0.15 may be prepared by mixing a reducing gas having a C/H of 0.15 or more with hydrogen gas.
  • the reducing gas mixed with the hydrogen gas may be any reducing gas having C/H of 0.15 or more, such as COG, natural gas, furnace top exhaust gas, and city gas described above. Etc.
  • the method for producing the reducing gas is not necessarily limited to this method. May be prepared by mixing a small reducing gas).
  • the graphs L2 to L5 are convex graphs, they are represented by a quadratic equation of the carbon consumption rate in the reducing gas.
  • X is a carbon unit in the reducing gas
  • Y is Input ⁇ C.
  • the shapes of the graphs L2 to L5 differ depending on the C/H of the reducing gas, at least one of the coefficients a2, b2, c2 is represented by a function including the C/H of the reducing gas as a variable.
  • the reducing agent ratio can be further reduced. It should be noted that the reason why the graphs L2 to L5 start to decrease after reaching the maximum value is that the carbon intensity in the reducing gas is excessively supplied as compared with the amount required for in-reactor reduction as described above. However, if the pre-tuyere temperature is constant, the oxygen enrichment rate will increase as the reducing gas injection rate increases. However, it is conceivable that the amount of gas blown into the blast furnace via the hot blast stove decreases and the sensible heat of the blast decreases.
  • the C/H of the reducing gas is preferably 0.13 or less, more preferably 0.10 or less, and even more preferably 0.05 or less.
  • the lower limit of C/H is not particularly limited and may be more than 0.
  • the ⁇ C-reducing gas correlation is less than 0.15 when the molar ratio C/H of carbon atoms and hydrogen atoms in the reducing gas is 0.15 or more.
  • the ⁇ C-reducing gas correlation is uniquely determined regardless of the type of the reducing gas (in other words, regardless of the C/H of the reducing gas). ..
  • the ⁇ C-reducing gas correlation differs for each C/H of the reducing gas.
  • the correlation between Input ⁇ C and the carbon intensity in the reducing gas is shown by a convex graph (that is, when the carbon intensity in the reducing gas has a certain value). Shows the maximum value).
  • the reducing gas is adjusted so that Input ⁇ C becomes equal to or higher than a predetermined target value based on the correlation.
  • the carbon intensity inside can be determined.
  • the blowing amount of the reducing gas blown into the blast furnace can be adjusted based on the determined carbon intensity in the reducing gas and the carbon ratio in the reducing gas.
  • a desired Input ⁇ C that is, Input ⁇ C equal to or larger than the target value
  • the ⁇ C-reducing gas correlation is created by performing the blast furnace operation simulation, but the method of creating the ⁇ C-reducing gas correlation is not limited to this.
  • the operation in the actual furnace including the actual operation and the test operation
  • the test operation in the test blast furnace by calculating the Input ⁇ C while changing the carbon intensity in the reducing gas, ⁇ C-reducing gas Correlation can be obtained.
  • a ⁇ C-reducing gas correlation is obtained for each C/H of reducing gas.
  • the method of obtaining the ⁇ C-reducing gas correlation is not particularly limited, but may be produced by, for example, performing a blast furnace operation simulation.
  • a blast furnace operation simulation for example, Koji TAKATANI, Takanobu INADA, Yutaka UJISAWA, “Three-dimensional Dynamic for Blast Furnace”, ISIJ International, V.I. 39 (1999), No. 1, p.
  • a so-called "blast furnace mathematical model” shown in 15-22 and the like can be used.
  • This blast furnace mathematical model roughly defines multiple meshes (small areas) by dividing the internal area of the blast furnace in the height direction, the radial direction, and the circumferential direction, and simulates the behavior of each mesh. is there.
  • the calculation conditions of the blast furnace operation simulation are not particularly limited, but it is preferable that the calculation conditions are in accordance with the actually executed operation conditions.
  • the tuyere temperature is preferably 2000° C. or higher.
  • the ⁇ C-reducing gas correlation hardly changes even if the front tuyere temperature changes.
  • the ⁇ C-reducing gas correlation is obtained for each C/H. That is, a graph showing the ⁇ C-reducing gas correlation is prepared.
  • the ⁇ C-reducing gas correlation shows different tendencies when the C/H of the reducing gas is 0.15 or more and when it is less than 0.15. Therefore, it is preferable to obtain a plurality of ⁇ C-reducing gas correlations in each case.
  • a blast furnace operation simulation will be performed in various cases where the reducing gas C/H and the blowing amount (blowing amount per ton of hot metal) are different.
  • This case also includes the base operation (operation in which the amount of reducing gas blown is 0).
  • at least one or more of the amount of air blown in the hot air and the oxygen enrichment ratio may be adjusted.
  • At least one of the coke ratio and the pulverized coal ratio may be adjusted.
  • the input ⁇ C and the carbon intensity in the reducing gas are calculated for each case.
  • the points indicating the Input ⁇ C and the carbon intensity in the reducing gas in each case are plotted on the xy plane shown in FIG. 1, for example.
  • Points P1 to P8 are examples of plotted points.
  • the approximation curve of each plot is obtained by an approximation method such as the least square method.
  • These approximate curves are graphs showing the ⁇ C-reducing gas correlation.
  • Graphs L1 to L5 are examples of graphs showing the ⁇ C-reducing gas correlation.
  • the carbon basic unit in the reducing gas that is equal to or higher than the predetermined target value of Input ⁇ C is determined. That is, the ⁇ C-reducing gas correlation corresponding to the C/H of the actually used reducing gas is selected, and based on the selected ⁇ C-reducing gas correlation, reduction that is not less than the target value of Input ⁇ C is performed. Determine the carbon intensity in the gas.
  • the C/H of the reducing gas may be obtained, for example, by specifying the composition of the reducing gas by the above-described measurement method and based on the specified composition of the reducing gas.
  • the ⁇ C-reducing gas correlation is shown by a graph that is convex upward. Therefore, it is preferable to determine the carbon unit consumption in the reducing gas near the maximum value of Input ⁇ C. Thereby, the reducing material ratio can be further reduced.
  • the C/H of the actually used reducing gas is 0.15 or more, it is preferable to determine the carbon basic unit in the reducing gas within the range of 21 to 107 kg/t-pig and 21 to 65 kg/ It is more preferable to determine the carbon unit consumption in the reducing gas within the range of t-pig. The reason is as described above.
  • Input ⁇ C can be set to a value of 4.0% or more. Further, by determining the carbon intensity of the reducing gas within the range of 21 to 65 kg/t-pig, the input ⁇ C can be increased (specifically, 4.0% or more with a smaller amount of the reducing gas blown in). And) Further, even if the carbon ratio in the reducing gas is small (particularly, the carbon ratio is less than 0.6 kg/Nm 3 ), the input ⁇ C is increased and the pre-tuyere temperature is stabilized at a predetermined value or higher. Can be maintained.
  • the front tuyere temperature tends to decrease as described above. Therefore, it is preferable to adjust the operating parameters including the oxygen enrichment rate so that the front tuyere temperature becomes a predetermined value (for example, 2000° C.) or more. Further, since the input ⁇ C decreases in the range of this set value, the carbon consumption rate in the reducing gas is excessively supplied as compared with the amount required for the reduction in the furnace, and the gas utilization rate decreases. Therefore, it is possible to take measures to improve the gas utilization rate, for example, to change the iron-based raw material to one having excellent reducibility.
  • the amount of reducing gas blown into the blast furnace (for example, per ton of hot metal) Adjust the blow rate).
  • the blowing amount of the reducing gas can be obtained by dividing the carbon consumption rate in the reducing gas by the carbon ratio in the reducing gas.
  • the blowing amount of the reducing gas is the value determined in the third step.
  • the reducing gas may be any one or more selected from the group consisting of COG, natural gas, a gas obtained by reforming a furnace top exhaust gas (BFG), and city gas, for example.
  • the reducing gas may be a mixed gas of these gases, or may be a mixture of these gases (including mixed gas) with hydrogen gas.
  • the reducing gas having a C/H of less than 0.15 may be produced by mixing hydrogen gas with COG or the like.
  • the reducing gas may be blown into the blast furnace without heating, but it is preferable to blow it into the blast furnace after heating. By heating the reducing gas and then blowing it into the blast furnace, a further reduction of the reducing material ratio can be expected.
  • the heating temperature is preferably about 300 to 350°C.
  • the tuyere for blowing the reducing gas into the blast furnace (hereinafter, also referred to as "reducing gas tuyere") is provided, for example, in the Bosch portion.
  • the reducing gas tuyere may be provided on the shaft portion.
  • Reducing gas tuyere may be provided on both the shaft portion and the Bosch portion.
  • the reducing gas blown from the shaft portion preferably contains a large amount of CO and/or H 2 , and is blown while controlling C/H.
  • Hot air is blown into the blast furnace as in the conventional blast furnace operation.
  • the temperature, composition and blowing amount of hot air may be the same as in conventional blast furnace operation.
  • the hot air includes air and may further include moisture and enriched oxygen.
  • the hot air is blown into the blast furnace from, for example, tuyere provided in the Bosch portion.
  • the tuyere for blowing hot air into the blast furnace may be the same as or different from the tuyere for reducing gas.
  • the carbon intensity in the reducing gas that is equal to or higher than the target value of Input ⁇ C is determined based on the previously determined ⁇ C-reducing gas correlation, and the carbon concentration in the determined reducing gas is determined.
  • the blowing amount of the reducing gas is determined based on the carbon intensity and the carbon ratio in the reducing gas. Therefore, the desired Input ⁇ C can be realized relatively reliably. That is, it is possible to obtain a desired effect of reducing the reducing agent ratio, and thus it is possible to more reliably reduce the reducing agent ratio. As a result, the CO 2 emission amount can be reduced.
  • Input ⁇ C shows a maximum value when the carbon intensity in the reducing gas has a certain value (this value differs for each C/H). Therefore, the reducing agent ratio can be further reduced by setting the set value of the carbon consumption rate in the reducing gas in the vicinity of this maximum value. Furthermore, if the above correlation is obtained for each C/H, then the amount of reducing gas blown can be determined and managed based on the above correlation corresponding to the C/H of the reducing gas. Therefore, it is possible to appropriately design and manage the operating specifications necessary for increasing Input ⁇ C.
  • Example 1> In Example 1, by performing a blast furnace operation simulation, it was confirmed that the above-mentioned ⁇ C-reducing gas correlation exists when C/H was 0.15 or more.
  • blast furnace mathematical model For the blast furnace operation simulation, the above-mentioned "blast furnace mathematical model" was used. The calculation conditions are shown in Table 3. All iron-based raw materials were sinter. The composition of the sinter was T-Fe:58.5%, FeO:7.5%, C/S:1.9, Al 2 O 3 :1.7%. As for coke, it was assumed that C: 87.2% and Ash: 12.6% were used (% represents mass%).
  • Example 1 the type of the reducing gas (that is, the value of C/H) and the blowing amount of the reducing gas (the blowing amount per ton of hot metal) were changed to perform the blast furnace operation simulation, and the above-mentioned ⁇ C- It was confirmed that there was a reducing gas correlation.
  • the reducing gas COG having the composition shown in Table 1 or natural gas having the composition shown in Table 2 was used.
  • the reducing gas was blown into the blast furnace from the tuyere provided in the Bosch part.
  • the air blowing amount and the oxygen enrichment rate in the hot air were adjusted so that the front tuyere temperature at the time of blowing the reducing gas was as constant as possible (that is, within the range shown in Table 3).
  • Example 2 In Example 2, by performing a blast furnace operation simulation, it was confirmed that the above-mentioned ⁇ C-reducing gas correlation exists when C/H was less than 0.15.
  • blast furnace mathematical model was used for the blast furnace operation simulation.
  • the calculation conditions were the same as in Example 1. Further, it was assumed that the same iron-based raw material and coke as in Example 1 were used.
  • Example 2 the reducing gas C/H and the reducing gas blowing amount (the blowing amount per ton of hot metal) were changed to perform the blast furnace operation simulation, and the above-mentioned ⁇ C-reducing gas correlation exists. It was confirmed.
  • the C/H of the reducing gas can be adjusted, for example, by mixing COG having the composition shown in Table 1 and hydrogen gas at different mixing ratios for each Case.
  • the reducing gas was blown into the blast furnace from the tuyere provided in the Bosch part.
  • the air blowing amount and the oxygen enrichment rate in the hot air were adjusted so that the front tuyere temperature at the time of blowing the reducing gas was as constant as possible (that is, within the range shown in Table 3).
  • the coke ratio was adjusted so that the hot metal temperature was constant in all cases.
  • the pulverized coal ratio was 115 kg/t-pig, and the blowing temperature was 1000° C., which were fixed conditions.
  • the calculation results are shown in Table 5 and FIG.

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  • Manufacturing & Machinery (AREA)
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  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Manufacture Of Iron (AREA)
  • Blast Furnaces (AREA)

Abstract

Un procédé de fonctionnement d'un haut-fourneau selon un aspect de la présente invention comprend les étapes consistant à : déterminer au préalable la corrélation entre une intensité de carbone dans un gaz réducteur et une quantité de réduction d'intensité de consommation de carbone ∆C à l'entrée due au soufflage du gaz réducteur dans un haut-fourneau pour chaque rapport molaire C/H entre l'atome de carbone et l'atome d'hydrogène dans le gaz réducteur ; déterminer une intensité de carbone qui devient égale ou supérieure à une valeur cible prédéterminée pour la quantité de réduction d'intensité de consommation de carbone ∆C à l'entrée dans le gaz réducteur sur la base de la corrélation qui a été déterminée pour chaque rapport molaire C/H ; et ajuster la quantité de soufflage du gaz réducteur à souffler dans le haut-fourneau sur la base de l'intensité de carbone dans le gaz réducteur qui a été déterminée dans l'étape de traitement et du rapport de teneur en carbone dans le gaz réducteur.
PCT/JP2020/006011 2019-02-18 2020-02-17 Procédé de fonctionnement d'un haut-fourneau Ceased WO2020171008A1 (fr)

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AU2020226229A AU2020226229B2 (en) 2019-02-18 2020-02-17 Blast furnace operation method
UAA202104860A UA127367C2 (uk) 2019-02-18 2020-02-17 Спосіб експлуатації доменної печі
US17/430,657 US12180555B2 (en) 2019-02-18 2020-02-17 Blast furnace operation method
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20230046067A (ko) 2021-09-29 2023-04-05 현대제철 주식회사 고로 조업 제어방법
JP2025500705A (ja) * 2022-01-12 2025-01-09 新疆八一▲鋼▼▲鉄▼股▲ふん▼有限公司 酸素富化型高炉操業方法
JP2025500704A (ja) * 2022-01-12 2025-01-09 新疆八一▲鋼▼▲鉄▼股▲ふん▼有限公司 超高酸素富化型低炭素製錬方法

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP7662417B2 (ja) * 2021-05-28 2025-04-15 日本製鉄株式会社 高炉の操業方法
JP7791433B2 (ja) * 2021-11-01 2025-12-24 日本製鉄株式会社 高炉の操業方法
US20240303751A1 (en) * 2023-03-07 2024-09-12 North China University Of Science And Technology Method for Predicting Carbon Consumption and Carbon Emission of Hydrogen-Rich Blast Furnace (BF) Based on C-rd Theory
TWI906913B (zh) * 2023-06-21 2025-12-01 日商日本製鐵股份有限公司 高爐的作業方法
JP7709109B1 (ja) * 2023-11-06 2025-07-16 日本製鉄株式会社 高炉の操業方法

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4198228A (en) * 1975-10-24 1980-04-15 Jordan Robert K Carbonaceous fines in an oxygen-blown blast furnace
JPS6019893B2 (ja) 1979-09-26 1985-05-18 イスチツ−ト・ビオロジコ・ケミオテラピコ（ア・ビ・チ）エツセ・ピ・ア 抗潰瘍剤
JP2007169750A (ja) 2005-12-26 2007-07-05 Jfe Steel Kk 高炉操業方法
JP2012520939A (ja) * 2009-03-17 2012-09-10 アルセロルミタル・インベステイガシオン・イ・デサロジヨ・エセ・エレ 高炉ガスを再循環させる方法、および関連装置
JP5070706B2 (ja) 2005-01-31 2012-11-14 Ｊｆｅスチール株式会社 高炉操業方法
JP2015129325A (ja) * 2014-01-07 2015-07-16 新日鐵住金株式会社 高炉の操業方法
JP2015199984A (ja) * 2014-04-08 2015-11-12 新日鐵住金株式会社 高炉の操業方法
JP2016113677A (ja) * 2014-12-16 2016-06-23 新日鐵住金株式会社 高炉の操業方法
JP2019026220A (ja) 2017-08-03 2019-02-21 井関農機株式会社 作業車両

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2719083A (en) * 1954-08-02 1955-09-27 Edmund S Pomykala Smelting method
JPS491686B1 (fr) * 1969-05-28 1974-01-16
JPS5070706U (fr) 1973-10-26 1975-06-23
DE2710106B2 (de) 1977-03-08 1980-08-14 Eisenwerk-Gesellschaft Maximilianshuette Mbh, 8458 Sulzbach-Rosenberg Verfahren zur Erzeugung von flüssigem Roheisen
JPS6019893U (ja) 1983-07-18 1985-02-12 ティーディーケイ株式会社 管路ヒ−タ
US5234490A (en) * 1991-11-29 1993-08-10 Armco Inc. Operating a blast furnace using dried top gas
RU2277127C1 (ru) * 2005-01-17 2006-05-27 Государственное образовательное учреждение высшего профессионального образования "Уральский государственный технический университет - УПИ" Способ вдувания горячих восстановительных газов в доменную печь
JP4984396B2 (ja) 2005-01-31 2012-07-25 Ｊｆｅスチール株式会社 高炉操業方法
DE102005027158A1 (de) * 2005-06-11 2006-12-28 Klaus Dr.-Ing. Scheidig Verfahren zu Erzeugung von Roheisen im Hochofen unter Zuführung von Reduktionsgas in den Hochofenschacht
JP6019893B2 (ja) 2012-07-31 2016-11-02 Ｊｆｅスチール株式会社 高炉の操業方法
DE102014216336A1 (de) * 2014-08-18 2016-02-18 Küttner Holding GmbH & Co. KG Verfahren zum Einblasen von Ersatzreduktionsmitteln in einen Hochofen
KR101758521B1 (ko) * 2015-12-23 2017-07-17 주식회사 포스코 열풍로를 이용한 이산화탄소 분해 및 재활용 방법
KR102135521B1 (ko) * 2016-02-05 2020-07-17 닛폰세이테츠 가부시키가이샤 고로 샤프트부로의 수소 함유 환원 가스 공급 방법
DE102017006067A1 (de) * 2017-06-27 2018-12-27 Helmut Aaslepp Sauerstoff-Hochofen mit Top Gas Recycling

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4198228A (en) * 1975-10-24 1980-04-15 Jordan Robert K Carbonaceous fines in an oxygen-blown blast furnace
JPS6019893B2 (ja) 1979-09-26 1985-05-18 イスチツ−ト・ビオロジコ・ケミオテラピコ（ア・ビ・チ）エツセ・ピ・ア 抗潰瘍剤
JP5070706B2 (ja) 2005-01-31 2012-11-14 Ｊｆｅスチール株式会社 高炉操業方法
JP2007169750A (ja) 2005-12-26 2007-07-05 Jfe Steel Kk 高炉操業方法
JP2012520939A (ja) * 2009-03-17 2012-09-10 アルセロルミタル・インベステイガシオン・イ・デサロジヨ・エセ・エレ 高炉ガスを再循環させる方法、および関連装置
JP2015129325A (ja) * 2014-01-07 2015-07-16 新日鐵住金株式会社 高炉の操業方法
JP2015199984A (ja) * 2014-04-08 2015-11-12 新日鐵住金株式会社 高炉の操業方法
JP2016113677A (ja) * 2014-12-16 2016-06-23 新日鐵住金株式会社 高炉の操業方法
JP2019026220A (ja) 2017-08-03 2019-02-21 井関農機株式会社 作業車両

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
AKITOSHI SHIGEMI: "Ironmaking Handbook", CHIJINSHOKAN CO., LTD.
KOUJI TAKATANITAKANOBU INADAYUTAKA UJISAWA: "Three-dimensional Dynamic Simulator for Blast Furnace", ISIJ INTERNATIONAL, vol. 39, no. 1, 1999, pages 15 - 22

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20230046067A (ko) 2021-09-29 2023-04-05 현대제철 주식회사 고로 조업 제어방법
KR102607615B1 (ko) * 2021-09-29 2023-11-30 현대제철 주식회사 고로 조업 제어방법
JP2025500705A (ja) * 2022-01-12 2025-01-09 新疆八一▲鋼▼▲鉄▼股▲ふん▼有限公司 酸素富化型高炉操業方法
JP2025500704A (ja) * 2022-01-12 2025-01-09 新疆八一▲鋼▼▲鉄▼股▲ふん▼有限公司 超高酸素富化型低炭素製錬方法
JP7795641B2 (ja) 2022-01-12 2026-01-07 新疆八一▲鋼▼▲鉄▼股▲ふん▼有限公司 酸素富化型高炉操業方法

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